Blown and stripped biorenewable oils

ABSTRACT

A method for producing a blown and stripped biorenewable oil is provided. The method may include the steps of (a) heating a biorenewable oil to at least 90° C.; (b) exposing an oxygen containing stream to the heated oil to produce a blown oil having a viscosity of at least 40 cSt at 40° C.; (c) adding a base metal catalyst to the blown oil; and (d) stripping the blown oil from step (c) until the stripped oil has an acid value of from about 1 mg KOH/g to about 20 mg KOH/g; wherein the stripped oil from step (d) has a flash point of at least 220° C.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application claims the benefit of U.S. Application Ser. No.61/953,061 filed Mar. 14, 2014, the disclosure of which is incorporatedherein by reference.

TECHNICAL FIELD

This disclosure relates to blown and stripped biorenewable oils andmethods for making such oils.

BACKGROUND

Recent technical challenges facing the asphalt industry have createdopportunities for the introduction of agriculture-based products for theoverall performance enhancement of asphalt.

The predominant use of asphalt is in road pavement, which is generallymade up of 95% aggregate and 5% asphalt binder. Asphalt binder istypically made up of >95% bitumen and <5% additives that enhanceperformance. Crude asphalt (bitumen) is primarily derived from thebottoms of petroleum refining, which is approximately 3% of the barrelof crude oil, depending on the grade of the crude oil. However,petroleum companies are improving refining efficiency to meet increasingdemands for transportation fuels, which negatively impacts the qualityand quantity of bitumen available for asphalt production. With coldtemperatures, asphalt becomes brittle, resulting in cracking and waterpenetration, leading to freeze-thaw damage. With high temperatures,asphalt becomes softer, resulting in rutting with heavy traffic. Inshort, higher refining efficiency is leading to asphalt which issignificantly more brittle. Accordingly, asphalt modifiers are beingincorporated into asphalt to modify its performance properties invariable weather conditions.

SUMMARY

One embodiment provides a method for producing a blown and strippedbiorenewable oil. The method comprises the steps of (a) heating abiorenewable oil to at least 90° C., (b) exposing an oxygen containingstream to the heated oil to produce a blown oil having a viscosity of atleast 40 cSt at 40° C., (c) adding a base metal catalyst to the blownoil; and (d) stripping the blown oil from step (c) until the strippedoil has an acid value of from about 1 mg KOH/g to about 20 mg KOH/g. Inthis embodiment, the stripped oil from step (d) has a flash point of atleast 220° C.

Another embodiment provides a method for producing a blown and strippedbiorenewable oil. The method comprises the steps of (a) heating acomposition comprising biorenewable oil and a first catalyst to at least90° C., (b) exposing an oxygen containing stream to the heatedcomposition from step (a) to produce a blown oil having a viscosity ofat least 40 cSt at 40° C., (c) adding a second catalyst to the blown oilfrom step (b), and (d) stripping the blown oil from step (c) to producea stripped oil having an acid value of from about 1 mg KOH/g to about 20mg KOH/g. In this embodiment, the first catalyst and the second catalystare different.

Another embodiment provides a method for producing a blown and strippedbiorenewable oil. The method comprises the steps of heating abiorenewable oil to at least 90° C., exposing an oxygen containingstream to the heated oil to produce a blown oil having a hydroxyl valueof 10 to 70, and stripping the blown oil from step (b) to produce astripped oil having an acid value of from about 1 mg KOH/g to about 20mg KOH/g.

Another embodiment provides a method for producing a blown biorenewableoil. The method comprises the steps of heating the oil to at least 90°C. and exposing an oxygen containing stream to the heated oil to producea blown oil having a viscosity of about 40 cSt to about 50 cSt at 40° C.The blown oil in this embodiment has a flash point of at least 220° C.

DETAILED DESCRIPTION

“Acid Value” (AV) is a measure of the residual hydronium groups presentin a compound and is reported in units of mg KOH/gram material. The acidnumber is measured according to the method of AOCS Cd 3d-63.

“Flash Point” or “Flash Point Temperature” is a measure of the minimumtemperature at which a material will initially flash with a brief flame.It is measured according to the method of ASTM D-92 using a ClevelandOpen Cup and is reported in degrees Celsius (° C.).

“Gardner Color Value” is a visual measure of the color of a material. Itis determined according to the procedure of ASTM D1544, “Standard TestMethod for Color of Transparent Liquids (Gardner Color Scale)”. TheGardner Color scale ranges from colors of water-white to dark browndefined by a series of standards ranging from colorless to dark brown,against which the sample of interest is compared. Values range from 0for the lightest to 18 for the darkest. For the purposes of theinvention, the Gardner Color Value is measured on a sample of materialat a temperature of 25° C.

“Iodine Value” (IV) is defined as the number of grams of iodine thatwill react with 100 grams of material being measured. Iodine value is ameasure of the unsaturation (carbon-carbon double bonds andcarbon-carbon triple bonds) present in a material. Iodine Value isreported in units of grams iodine (I₂) per 100 grams material and isdetermined using the procedure of AOCS Cd 1d-92.

“Hydroxyl Value” is a measure of the hydroxyl (—OH) groups present in amaterial. It is determined using the procedure of AOCS Cd 13-60.

“Performance Grade” (PG) is defined as the temperature interval forwhich a specific asphalt product is designed. For example, an asphaltproduct designed to accommodate a high temperature of 64° C. and a lowtemperature of −22° C. has a PG of 64-22.

“Pour Point” or “Pour Point Temperature” is a measure of the lowesttemperature at which a fluid will flow. It is measured according to themethod of ASTM D-97 and is reported in degrees Celsius (° C.).

“Useful Temperature Interval” (UTI) is defined as the interval betweenthe highest temperature and lowest temperature for which a specificasphalt product is designed. For example, an asphalt product designed toaccommodate a high temperature of 64° C. and a low temperature of −22°C. has a UTI of 86. For road paving applications, the seasonal andgeographic extremes of temperature will determine the UTI for which anasphalt product must be designed.

Also, for the purpose of this invention, asphalt, asphalt binder, andbitumen refer to the binder phase of an asphalt pavement. Bituminousmaterial may refer to a blend of asphalt binder and other material suchas aggregate or filler. The binder used in this invention may bematerial acquired from asphalt producing refineries, flux, refineryvacuum tower bottoms, pitch, and other residues of processing of vacuumtower bottoms, as well as oxidized and aged asphalt from recycledbituminous material such as reclaimed asphalt pavement (RAP), andrecycled asphalt shingles (RAS).

Biorenewable Oils

Biorenewable oils are used as the starting oil material. Biorenewableoils can be include oils isolated from plants, animals, andmicroorganisms including algae.

Plant-based oils are oils recovered from plants and algae. Plant-basedoils that can be utilized in the invention include, soybean oil, linseedoil, canola oil, rapeseed oil, cottonseed oil, sunflower oil, palm oil,peanut oil, safflower oil, corn oil, corn stillage oil, lecithin(phospholipids) and combinations and crude streams thereof orco-products, by-products, or residues resulting from oil refiningprocesses.

Examples of animal-based oils may include but are not limited to animalfat (e.g., lard, tallow) and lecithin (phospholipids), and combinationsand crude streams thereof

Biorenewable oils can also include partially hydrogenated oils, oilswith conjugated bonds, and bodied oils wherein a heteroatom is notintroduced, including diacylglycerides, monoacylglycerides, free fattyacids, and alkyl esters of fatty acids (e.g., methyl, ethyl, propyl, andbutyl esters).

Biorenewable oils can also include derivatives thereof, for example,previously modified or functionalized oils (intentional orunintentional) wherein a heteroatom (oxygen, nitrogen, sulfur, andphosphorus) has been introduced may also be used as the starting oilmaterial. Examples of unintentionally modified oils are used cookingoil, trap grease, brown grease, or other used industrial oils. Examplesof previously modified oils are those that have been previouslyvulcanized or polymerized by other polymerizing technologies, such asmaleic anhydride or acrylic acid modified, hydrogenated,dicyclopentadiene modified, conjugated via reaction with iodine,interesterified, or processed to modify acid value, hydroxyl number, orother properties. Such modified oils can be blended with unmodifiedplant-based oils or animal-based oils, fatty acids, glycerin, and/orgums materials.

Due to its relatively low polyunsaturation levels, relatively high mono-and di-unsaturation levels and other properties as further describedbelow, the preferred plant oil utilized for the invention is cornstillage oil (also known as recovered corn oil), or alternatively ablend of corn stillage oil with other oils, such as soybean or palm oil.The preferred oil to blend with corn stillage oil is soybean oil becauseof soybean oil's relatively higher level of polyunsaturates compared tocorn stillage oil. If higher functionality is desired, biorenewable oilshaving higher levels of unsaturation can be used. Conversely highersaturates may be incorporated to further vary solvent parameters of thepolymerized oils to improve performance properties in asphalt.

Corn-Stillage Oil

The inventors have surprisingly discovered that the monoglycerides,diglycerides, triglycerides, free fatty acids, and glycerol (hereinaftercollectively referred to as “corn stillage oil” which may also bereferred to as “recovered corn oil”) can be recovered from the otherresidual liquids resulting from the distillation of dry-grind cornfermented mash by suitable means, preferably by centrifugation of theresidual material remaining after the ethanol has been distilled offCentrifugation typically recovers twenty five percent of the cornstillage oil originally present in the residual material beingcentrifuged.

The corn stillage oil recovered by centrifugation typically: has an acidvalue from 16 to 32 mg KOH/gram, preferably from 18 to 30 mg KOH/gram;has an iodine value from 110 to 120 g I₂/100 g sample; and contains from0.05 to 0.29 percent by weight monoglycerides, from 1.65-7.08 percent byweight diglycerides, from 70.00 to 86.84 percent by weighttriglycerides, from 8 to 16 percent by weight (for example, from 9 to 15percent by weight) free fatty acids, and from 0.00 to 0.20 weightpercent glycerin. Typically, the corn stillage oil has from 53 to 55percent by weight groups derived from diunsaturated fatty acids, from 39to 43 percent by weight groups derived from monounsaturated fatty acids,from 15 to 18 percent by weight groups derived from saturated fattyacids, and from 1 to 2 percent by weight groups derived fromtriunsaturated fatty acids. The groups derived from each of the abovefatty acids are present either as groups within the mono-, di-, andtri-glycerides or as free fatty acids.

The free fatty acid content of the corn stillage oil most commonly isfrom about 11 to 12 percent (an acid value of from about 22 to 24 mgKOH/gram) is very high compared to conventional vegetable oils, but asmentioned above, the free fatty acid content can be higher or lowerdepending on processing procedure.

Recovery of Corn & Wage Oil

Fermented mash comprising ethanol, water, residual grain solids(including proteins, fats, and unfermented sugars and carbohydrates),and from 1 to 3 percent by weight corn stillage oil is heated to distilland recover ethanol from the fermented mash.

After the ethanol is distilled off, the remaining liquid portiontypically contains from 1 wt % to 4 wt % corn stillage oil. The materialremaining after the ethanol is distilled off is typically centrifugedusing a centrifuge, such as a Westfalia sliding disk centrifugeavailable from Westfalia Corporation. From 25 wt % to 35 wt % of thecorn stillage oil contained in the material is recovered during thiscentrifugation step. The recovered unprocessed corn stillage oiltypically exhibits a Gardner color of 12 or greater, for example, aGardner color of from 14 to 18.

Unprocessed corn stillage oil typically exhibits: a viscosity at 40° C.of from 25 to 35 cSt (for example from 28 to 31 cSt) as measuredutilizing viscosity tubes in a constant temperature bath as furtherdescribed below; a viscosity at 100° C. of from 5 to 10 cSt for examplefrom 6 to 9 cSt as measured utilizing viscosity tubes in a constanttemperature bath as further described below; a Viscosity Index of from80 to 236 determined using the procedures and measurement scaleestablished by the Society of Automotive Engineers; a flash point from220° C. to 245° C., for example from 225° C. to 240° C.; asaponification value of from 170 to 206 mg KOH/g; a pour point typicallyof from −5° C. to −14° C.; an acid value of from 15 to 33 mg KOH/gram(for example, from 16 to 32 mg KOH/gram); an iodine value from 110 to125 grams I₂/100 grams sample; and from 8 to 16 wt % (for example, from9 to 15 wt %) free fatty acids.

Viscosity for this invention is measured according to the method of ASTMD445. In this method oil to be tested is placed in a calibrated glasscapillary viscometer, which is then placed into a constant temperaturebath at the temperature specified. Once thermal equilibrium is reached,the oil is drawn up into the reservoir of the capillary tube. As thefluid drains, it passes the top mark on the tube and a timer is started.When the oil passes the lower mark, the timer is stopped and the flowtime is recorded. The recorded flow time is multiplied by a factor whichis specific to each viscometer tube. The resultant product of the flowtime multiplied by the factor is reported as viscosity in cSt at thetest temperature.

Unprocessed corn stillage oil also typically contains two phases at 25°C. The first phase is the liquid phase, which settles toward the top ofany container that contains the corn stillage oil. This phase typicallyis reddish in color. The second phase is a solid that typically settlestoward the bottom of any container containing the oil. At 62° C., thesecond phase tends to dissolve into the liquid phase, but will settleout again if the untreated corn stillage oil is cooled to roomtemperature. The inventors have determined that the second solid phasetypically makes up at least 4 percent by weight (4 wt %) of the totalunprocessed corn stillage oil. For example, the second solid phase maymake up from 5 wt % to 12 wt % of the unprocessed corn stillage oil. Forpurposes of this invention, this second solid phase is referred to asthe “titre.”

Heating the Oil

The biorenewable oil is heated to at least about 90° C., and preferablyfrom about 100° C. to about 115° C. It shall be understood that thisheating temperature may increase, for example to 160° C. or greater, toachieve faster polymerization. As described above, the biorenewable oilmay include, for example, soybean oil, linseed oil, canola oil, rapeseedoil, cottonseed oil, sunflower oil, palm oil, peanut oil, safflower oil,corn oil, corn stillage oil, or combinations thereof. In a preferredembodiment, however, the biorenewable oil is corn stillage oil, soybeanoil, or combinations thereof.

In some aspects, the biorenewable oil comprises from about 10% to about15% by weight free fatty acids, from about 12% to about 20% by weightdiacylglycerides, and from about 65% to about 78% by weighttriglycerides.

Additives, initiators, catalysts, or combinations thereof, may be addedto the biorenewable oil. Additives such as lecithin and/or additionalfatty acids may be added to the biorenewable oil before or during theheating step. The use of additives may aid in reduction of costsassociated with the biorenewable oil while at the same time providingadditional benefit of surfactancy and thus superior applicationperformance, specifically benefitting emulsifiability, anti-strip, andwarm mix lubricity. Initiators such as peroxide or lung oil may be addedto the biorenewable oil before or during the heating step.

A base metal catalyst also may be added to the biorenewable oil beforeor during the heating step to aid in the subsequent blowing step. If abase metal catalyst is used, it comprises a transition metal, and thetransition metal is selected from the group consisting of cobalt, iron,zirconium, lead, and combinations thereof. The base metal catalyst maybe added in amounts ranging from 200-1000 ppm.

In another aspect, accelerators may also be added to the biorenewableoil. For example, oxidizing chemicals, such as persulfates andpermanganates, may be added to the biorenewable oil. In the presence ofoxygen (from the oxygen containing stream, described below), theseoxidizers (which promote oxidation) accelerate oxidative polymerization.

Blowing the Oil

Blowing is typically achieved by passing or exposing an oxygencontaining stream through or to, respectively, the heated biorenewableoil or a composition comprising the biorenewable oil and othercomponents (e.g., additives, initiators, catalysts). It shall beunderstood however that other processes that enable oxidation may beused as well to achieve a similar result as the blowing process. Thevessel containing the biorenewable oil during the blowing step typicallyoperates at atmospheric pressure. The pressure of the oxygen containingstream being blown through the oil is generally high enough to achievethe desired air flow through the biorenewable oil. The oxygen containingstream is introduced at a sufficient flow rate for a sufficient periodof time to achieve the desired viscosity. Typically, the oxygencontaining stream is introduced into the biorenewable oil at a rate offrom about 40 to 450 cubic feet per minute. Preferably, the oxygencontaining stream is dispersed evenly in the vessel to maximize surfacearea exposure. Typically, the vessel will have a distribution ring orspoke-like header to create small volume bubbles evenly within the oil.The duration of blowing the oxygen containing stream through the oil isvaried and determined according to the desired properties of the blownoil and the end-use application for the resulting product.

In one aspect, the oxygen containing stream is an oxygen enriched streamderived from air. In another aspect, the oxygen containing streamcomprises air. In yet another aspect, the oxygen containing streamcomprises hydrogen peroxide.

The oxygen containing stream is blown through the biorenewable oil toprovide a blown oil which has a viscosity of at least about 40 cSt at40° C. to about 70 cSt at 40° C., and more preferably a viscosityranging from about 40 cSt at 40° C. to about 60 cSt at 40° C., and evenmore preferably a viscosity ranging from about 40 cSt at 40° C. to about55 cSt at 40° C. It shall be understood that for some biorenewablematerials may be in solid form at 40° C., accordingly the viscositymeasurement may need to be measured at higher temperatures.

The blown oil produced may comprise from about 10% to about 15% byweight free fatty acids, from about 12% to about 20% by weightdiacylgycerides, from about 50% to about 70% by weight triglycerides,and from about 5% to about 20% by weight dimers (wherein dimers aredefined as compounds having a molecular weight ranging from about1500-2000 g/mol) and trimers (wherein trimers are defined as having amolecular weight ranging from about 2300-3000 g/mol), collectively.

The reactions that occur during the blowing of the oil increase themolecular weight of the oil, which tends to increase the viscosity ofthe blown oil versus the unblown oil. Additionally, the blowing processintroduces hydroxyl and peroxide functionality into the resulting oil,which also tends to increase the viscosity of the oil.

In certain aspects where there is little to no concern for a desiredacid value or flash point, the method can stop after blowing withoutproceeding to the stripping step. In this case, a primary focus of theblowing is to carry out etherification.

Stripping the Oil

The blown biorenewable oil can be stripped using a nitrogen sparge and,optionally, under vacuum conditions.

Before the blown biorenewable oil is stripped, however, a base metalcatalyst may be added to the blown biorenewable oil to enhance thestripping step. In preferred aspects, the base metal catalyst is addedin an amount ranging from 250-1200 ppm, and more preferably ranging from900-1100 ppm. The amount of catalyst is controlled in such a way toprovide the optimum level of fatty soaps in the final product.

In one aspect, the base metal catalyst comprises metal selected from thegroup consisting of monovalent metals, divalent metals, and combinationsthereof as described in the IUPAC Periodic Table of Elements (2013). Inother aspects, the base metal catalyst comprises metals selected fromthe group consisting of potassium, calcium, sodium, magnesium andmixtures thereof. In preferred aspects, the base metal catalyst ispotassium hydroxide. The catalyst added to the blown biorenewable oilbefore the stripping step is not the same as the optional catalyst addedto the biorenewable oil before the blowing step.

Typically, the temperature during the stripping step ranges from about230° C. to about 350° C., and in some aspects from 230° C. to about 270°C., and in other aspects from about 235° C. to about 245° C. Thestripping step typically increases molecular weight and therefore raisesthe viscosity of the oil. The stripping will also lower the content offree fatty acids in the oil and remove other volatiles from the oil,therefore reducing the acid value of the resulting stripped oil.

During the initial stages of the stripping step, bodying reactions mayalso take place. Notably, after a biorenewable oil is blown, it maycarry with it dissolved oxygen and residual peroxides. These peroxidescontinue to react via oxidative polymerization as the fluid is heateduntil the existing supply of peroxide is consumed or decomposed by theelevated temperature. A nitrogen sparge is preferably introduced with asparge rate high enough to assist in the removal of the volatiles. Insome aspects, a vacuum can be used during the stripping step. The spargerate is maintained on the oil to assist in the removal of volatiles fromthe oil, including water that may be liberated by the reaction ofglycerin with fatty acids (when polyols are added to the stripping step,which is further described below). Once the acid value has been reducedto the desired value, the heat may be removed if the desired viscosityhas been obtained. If the desired viscosity has not been reached, theoil can continue to be heated until the desired value for viscosity isobtained. After the desired acid value and viscosity have been obtained,the blown, stripped biorenewable oil may cool.

In preferred aspects, the blown oil is stripped until the acid value ofthe oil is reduced to from 1 mg KOH/gram to about 20 mg KOH/gram,preferably from about 2 mg KOH/gram to about 15 mg KOH/gram, and morepreferably from about 3 mg KOH/gram to about 9 mg KOH/gram. Further, theblown oil is stripped until the hydroxyl value of the strippedbiorenewable oil ranges from about 10 to about 70.

The inventors have surprisingly discovered that when it is necessary toreduce the acid value to particularly low levels (for example to valuesof 3.5 mg KOH/gram or less), it may be preferable to optionally addsmall amounts of a polyol (1.0-1.3% by weight of polyol—equivalent to2.5-3 mole ratio free fatty acid to I mole ratio polyol), preferablyglycerol, to the blown oil before, during, or after the stripping step.

Stripping the oil increases the viscosity of the resulting oil comparedto the non-stripped oil and will increase the flash point of theresulting oil. Thus, in some aspects, the viscosity of the stripped oilranges from about 45 eSt to about 70 eSt at 40° C. Further, in someaspects, the flash point of the resulting oil is at least 220° C., morepreferably at least 230° C., even more preferably at least 240° C., andeven more preferably at least 246° C. In other aspects, the flash pointof the resulting oil ranges from about 225° C. to about 245° C.

Further, in aspects of the present invention, the stripped biorenewableoil comprises from about 2% to about 10% by weight free fatty acids,from about 12% to about 22% by weight diacylglycerides, from about 50%to about 70% by weight triglycerides, and from about 5% to about 20% byweight dimers (wherein dimers are defined as compounds having amolecular weight ranging from about 1500-2000 g/mol) and trimers(wherein trimers are defined as having a molecular weight ranging fromabout 2300-3000 g/mol), collectively (it shall be understood that asmall amount of tetramers may also be included in that 5% to 20% range).

Polyol

As discussed above, the inventors have surprisingly discovered that byadding a polyol to the blown oil the blown oil may be more easilystripped to obtain a blown, stripped biorenewable oil having a highviscosity and a low acid value as described above, which will result ina blown, stripped biorenewable oil having a high flash point andsuperior asphalt performance (e.g., reducing short term age hardeningand volatile mass loss leading to enhanced UTI improvement, mitigationof deleterious interactions with asphalt additives, etc.).

The added polyol preferably has a molecular weight of at least 80Daltons, more preferably at least 85 Daltons, and more preferably atleast 90 Daltons. In order to aid in the reaction of the polyol with thefree fatty acids, the polyol preferably has at least two hydroxyl groupsper molecule, and more preferably at least 3 hydroxyl groups permolecule. The polyol preferably has a boiling point of at least 250° C.,more preferably at least 270° C., and further more preferably at least285° C. Any reference to boiling point herein means the boiling point ata pressure of 760 mm Hg. Due to its relatively high molecular weight (92Daltons), relatively high boiling point (290° C.), high number ofhydroxyl groups per molecule (3), and ready commercial availability,glycerin is the preferred polyol to utilize in the invention.

Examples of other polyols that may be utilized include, but are notlimited to, trimethylol propane (“TMP”), polyethylene glycol (“PEG”),pentaerythritol, and polyglycerol.

In certain preferred aspects of the invention, the polyol (e.g.glycerol) contains less than 500 ppm chloride ions. In certain aspects,the polyol contains less than 300 ppm, less than 200 ppm, less than 100ppm, less than 70 ppm, or less than 50 ppm chloride ions. Reducedchloride ion concentrations may minimize corrosion concerns in productsthat are manufactured utilizing a blown, stripped biorenewable oil ofthe present invention. In one particularly preferred aspect, the polyolcomprises technical grade or USP glycerol, typically having less than 30ppm chloride ions and preferably less than 20 ppm chloride ions (forexample less than 10 ppm chloride ions).

End-Use Applications Asphalt Modification

The declining quality of bitumen drives the need for adding chemicalmodifiers to enhance the quality of asphalt products. Heavy mineral oilsfrom petroleum refining are the most commonly used modifiers. Thesemineral oils extend the low temperature limit of the asphalt product by‘plasticizing’ the binder, however this also tends to lower the uppertemperature limit of the asphalt. The blown and stripped biorenewableoils described herein are not only viable substitutes for mineral oil,but have also been shown to extend the UTI of asphalts to a greaterdegree than other performance modifiers, therefore providing substantialvalue to asphalt manufacturers.

UTI of asphalt is determined by a series of standard tests developed bythe Strategic Highway Research Program (SHRP) AASHTO specifications.This is a unique property not seen in other asphalt softening additivessuch as asphalt flux, fuel oils, products based on aromatic ornaphthenic distillates, or flush oils. UTI increases for approximately3% by weight addition of the blown and stripped biorenewable oils,described herein, may be up to 4° C., therefore providing a broader PGmodification range such that the lower end temperature can be lowerwithout sacrificing the higher end temperature.

EXAMPLES

The following examples are presented to illustrate the present inventionand to assist one of ordinary skill in making and using same. Theexamples are not intended in any way to otherwise limit the scope of theinvention.

Example 1 Blowing the Corn Stillage Oil Using a Catalyst

In this example, a cobalt/calcium hydroxide catalyst is added to cornstillage oil before the blowing step. More specifically, 250 ppm ofcobalt and 250 ppm of calcium hydroxide is added to the corn stillageoil. The corn stillage oil is heated to 90-115° C. and subsequently, airis blown through the oil using a sparge ring or dip tube. The reactionis monitored for desired viscosity build.

A control experiment is also carried out that utilizes a similar methodbut without the use of the cobalt/calcium hydroxide catalyst. The amountof time it takes to achieve a desired viscosity in both thecobalt/calcium experiment and control experiment are compared againsteach other.

As demonstrated in Table 1, after an 8 and 12 hour period, the viscosityof the blown oil increased at a faster rate in the experiment with thecatalyst. In conclusion, using the catalyst improved the blowingreaction time by a factor of around 2.5 times that of the blowingreaction without the catalyst, therefore providing significant timesavings to achieve a desired viscosity.

TABLE 1 Control Cobalt/Calcium Catalyst Time (hrs) Viscosity (cSt) Time(hrs) Viscosity (cSt) 0 32 0 32 8 37.8 8 90.8 12 63 12 165 16 96

Example 2 Stripping Corn-Stillage Oil Using KOH Catalyst

In this example, about 1000 ppm of KOH catalyst is added to blown cornstillage oil. The blown corn stillage oil is heated to 230-235° C. andstripped using a nitrogen sparge. The reaction is monitored forreduction in acid value. A control experiment is also carried out thatutilizes a similar method but without the use of the KOH catalyst. Theeffect of the KOH catalyst during the stripping step is compared againsta control experiment having no catalyst.

As demonstrated in Table 2, the acid value of the stripped oil decreasesat a faster rate with the catalyst than without. Even after a 9 hourperiod, the acid value of the stripped oil without the use of a catalystdid not achieve the low acid value of the stripped oil using KOHachieved after a 5 hour period. Thus, the use of the catalyst decreasedthe stripping reaction time by a factor of at least 2 times that of thestripping reaction without the catalyst.

TABLE 2 Control KOH Catalyst Time (hrs) Acid Value Time (hrs) Acid Value0 20 0 20 3 9.6 3 6.6 4 7.7 4 5.4 5 6.6 5 3.6 6 6.2 7 5.6 8 5.3 9 4.3

Example #3 Effect of Free Fatty Acid Content

A set of samples were prepared in which different dosages of Oleic acid(C 18:1) was blended into a refined soybean oil. The purpose of theexperiment was to demonstrate the adverse effect of the free fatty acid(as represented by the added Oleic acid content in this example) on theflashpoint and aging characteristics of the oil. Table 3 shows theeffect of the added oleic acid on the open cup flashpoint:

TABLE 3 Added Oleic Acid Open cup Base Oil Content Content Flashpoint100% SBO   0% Added Oleic Acid 314° C. 90% SBO 10% Added Oleic Acid 242°C. 75% SBO 25% Added Oleic Acid 224° C. 45% SBO 55% Added Oleic Acid208° C.

Using the oil and oleic acid blends described above, a set of modifiedasphalt binder comprising the following was made:

-   -   97.0% by weight of neat asphalt binder graded as PG64-22 (PG        64.9-24.7)    -   The modifier blended into the asphalt after the binder had been        annealed at 150° C. for 1 hour.

Short term aging was performed using a Rolling Thin Film oven (RTFO) at163° C. for 85 minutes in accordance to ASTM D2872. The procedure isused to simulate the oxidation and volatilization that occurs in theasphalt terminal when the binder is heated and applied to the aggregate.The RTFO conditioning increases the complex modulus through oxidationand volatilization, as measured using the Dynamic Shear Rheometerparallel plate geometry (25 mm diameter, 1 mm gap) in accordance to ASTMD7175.

The results shown in Table 5 demonstrate a significant increase in theratio of |G*|/sin δ after aging to that before aging, indicating ahigher amount of “age hardening” in the asphalt binder as the free fattyacid content increased. The nearly linear relationship between theincrease in the oleic acid content and the increase volatile mass lossalso indicates the volatility of the oleic acid at the high temperatureand flow rates that the binder is exposed to during RTFO aging. Theseresults indicate the desirability of using low free fatty acid base oilsand stripping of the free fatty acid in oils with higher free fatty acidcontent. Furthermore, stripping to further reduce the free fatty acidcontent consequently reduces acid value which aids in preventingnegative reactions with amine antistrips.

TABLE 4 Unaged RTFO Aged Aging RTFO Base Oil Added Oleic Acid |G*|/sinδat |G*|/sinδ at 64° C. Ratio of Increase in Volatile Content Content 64°C. (kPa) (kPa) RTFO/Unaged |G*|/sinδ Mass Loss 100% SBO 0% Added Oleic0.56 1.33 2.37 137.1% 0.390% Acid 90% SBO 10% Added Oleic 0.54 1.33 2.46145.8% 0.457% Acid 75% SBO 25% Added Oleic 0.53 1.35 2.55 154.8% 0.545%Acid 45% SBO 55% Added Oleic 0.52 1.35 2.58 157.6% 0.688% Acid

For the purposes of this specification and appended claims, unlessotherwise indicated, all numbers expressing quantities, percentages orproportions, and other numerical values used in the specification andclaims, are to be understood as being modified in all instances by theterm “about.” Accordingly, unless indicated to the contrary, thenumerical parameters set forth in the following specification andattached claims are approximations that can vary depending upon thedesired properties sought to be obtained by the present disclosure. Atthe very least, and not as an attempt to limit the application of thedoctrine of equivalents to the scope of the claims, each numericalparameter should at least be construed in light of the number ofreported significant digits and by applying ordinary roundingtechniques.

It is noted that, as used in this specification and the appended claims,the singular forms “a,” “an,” and “the,” include plural referents unlessexpressly and unequivocally limited to one referent. Thus, for example,reference to “a meat” includes two or more different meats. As usedherein, the term “include” and its grammatical variants are intended tobe non-limiting, such that recitation of items in a list is not to theexclusion of other like items that can be substituted or added to thelisted items.

While particular embodiments have been described, alternatives,modifications, variations, improvements, and substantial equivalentsthat are or can be presently unforeseen can arise to applicants orothers skilled in the art. Accordingly, the appended claims as filed andas they can be amended are intended to embrace all such alternatives,modifications variations, improvements, and substantial equivalents.

1-32. (canceled)
 33. A method for producing a blown and strippedbiorenewable oil, the method comprising the steps of: (a) heating acomposition comprising biorenewable oil and a first catalyst to at least90° C.; (b) exposing an oxygen containing stream to the heatedcomposition from step (a) to produce a blown oil having a viscosity ofat least 40 cSt at 40° C.; (c) adding a second catalyst to the blown oilfrom step (b); and (d) stripping the blown oil from step (c) to producea stripped oil having an acid value of from about 1 mg KOH/g to about 20mg KOH/g; wherein the first catalyst and the second catalyst aredifferent.
 34. The method of claim 33, wherein the composition in step(a) is heated to about 115° C.
 35. The method of claim 33, wherein theoxygen containing stream is an oxygen enriched stream derived from air.36. (canceled)
 37. The method of claim 33, wherein the oxygen containingstream comprises hydrogen peroxide.
 38. The method of claim 33, whereinthe stripping step includes bodying reactions.
 39. The method of claim33, wherein the first catalyst is a base metal catalyst comprising atransition metal.
 40. (canceled)
 41. The method of claim 33, whereinstep (a) includes adding the first catalyst in an amount ranging fromabout 200 ppm to about 1000 ppm.
 42. The method of claim 33, wherein thecomposition in step (a) further comprises a peroxide initiator.
 43. Themethod of claim 33, wherein the composition in step (a) furthercomprises tung oil.
 44. The method of claim 33, the second catalystcomprises potassium hydroxide.
 45. The method of claim 33, wherein thesecond catalyst is a base metal catalyst.
 46. (canceled)
 47. The methodof claim 45, wherein the base metal catalyst comprises metal selectedfrom the group consisting of potassium, calcium, sodium, magnesium, andcombinations thereof.
 48. The method of claim 33, wherein step (c)includes adding the second catalyst in an amount ranging from about 250ppm to about 1200 ppm.
 49. (canceled)
 50. The method of claim 33,further including the step of adding a polyol to the stripped oilbefore, during, or after step (d).
 51. The method of claim 50, whereinthe polyol comprises glycerol,
 52. The method of claim 33, wherein theviscosity of the stripped oil produced in step (d) ranges from about 45cSt to about 70 cSt at 40° C.,
 53. The method of claim 33, wherein thestripped oil produced in step (d) comprises: (a) from about 2% to about10% by weight free fatty acids; (b) from about 12% to about 22% byweight diacylgycerides; (c) from about 50% to about 70% by weighttriglycerides; and (d) from about 5% to about 20% by weight dimers andtrimers content, collectively.
 54. The method of claim 33, wherein thestripped oil produced in step (d) has a flash point of at least 220° C.55-57. (canceled)
 58. The method of claim 33, wherein the stripped oilproduced in step (d) has a hydroxyl value of 10 to
 70. 59. (canceled)60. The method of claim 33, wherein the stripped oil produced in step(d) has an acid value of from about 1 mg KOH/g to about 20 mg KOH/g.61-82. (canceled)